Process for brominating polystyrenic resins

ABSTRACT

This invention features a process for brominating styrenic polymers which process comprises feeding a first stream comprising a brominating agent, a second stream comprising styrenic polymer and a third stream comprising bromination catalyst to a mixer to intimately mix such streams.

This application is a continuation of application Ser. No. 08/721,398,filed Sep. 26, 1996, now U.S. Pat. No. 5,686,538.

BACKGROUND OF THE INVENTION

This invention relates to an economical and safe process for producinghigh quality brominated polystyrenic resins.

Brominated polystyrenic resins, i.e., polymers containing alkenylaromatic repeating units, are useful flame retardants. Particularlyuseful are brominated polystyrenes, especially those containing at leastabout 60 wt % bromine. High value is placed on brominated polystyrenewhich has close to 70 wt % bromine and a near-white color. This highlyvalued product is not easily obtained as most processes are limited bythe inverse correlation between high bromine content and good color. Inaddition to obtaining a high bromine content and good color, thebrominated resin should have no or at least a very low degree ofcross-linking present.

Most processes for brominating styrenic polymers feature contacting abrominating agent, e.g., bromine, BrCl, and the like, with a solution ofthe styrenic polymer in the presence of a Lewis acid catalyst, such asAlCl₃, AlBr₃, FeCl₃, and FeBr₃. Using this basic model, the art has,over the years, strived to divine the best possible process. Success hasnot been easy as the various proposed processes have not fully fulfilledtheir promise.

U.S. Pat. No. 4,975,496 describes an intriguing process for brominatingstyrenic polymers to obtain a high quality product in good yields. Theprocess features contacting a solution of at least one styrenic polymerwith a brominating agent in the presence of a Lewis acid catalyst,wherein both the styrenic polymer and the brominating agent areseparately fed into contact with the Lewis acid catalyst. The '496patent stresses the importance of the separated feeds. When the catalystused is very active, say AlCl₃, it is also deemed critical to insure athorough dispersion of some of the brominating agent in the catalystbefore the styrenic polymer is fed. Thus, it is recommended that atleast 5 mole percent of the total brominating agent be pre-added to thereactor.

The '496 process, while it may be an improvement over the prior artprocesses, is not a panacea. In a study of the bromination ofpolystyrene, it was concluded that processes which use separatebrominating agent and polystyrene feeds, as is taught by the '496patent, run the danger of experiencing vapor eruptions which can causethe reactor contents to be splashed to the top of the reactor and/orinto the reflux and feed trains. It is believed that the intensity ofthese eruptions will be highest where the more active catalysts are usedand/or where the reaction conditions favor vigorous bromination. Also,it is predicted that the problem of vapor eruptions will be most seriousin commercial-size reactors, say from about 500 to about 6,000 gal.reactors, since such reactors cannot be, from a practical viewpoint, ashighly stirred as can be smaller reactors.

The vapor eruption is the result of poor heat and mass transfer. Whenthe brominating agent feed is separate from the styrenic polymer feedand the reactor is large and not highly stirred, there are goodopportunities for highly concentrated, large amounts of the tworeactants to meet. The resulting exothermic reaction, without good heattransfer, can cause vaporization of some of the reaction solvent. Also,the bromination reaction produces HBr as a gaseous by-product whichcontributes to the total vapor volume. When the combined vapor volume islarge and localized, there can be expected the above-mentioned eruption.

It is, therefore, an object of this invention to provide a process forbrominating styrenic polymers, which process is safe from vaporeruptions and which produces a brominated styrenic polymer havingexcellent color, high bromine content and little cross-linking.

THE INVENTION

This invention features a process for brominating, styrenic polymers,which process comprises feeding a first stream comprising a brominatingagent, a second stream comprising styrenic polymer, and a third streamcomprising bromination catalyst to a mixer to intimately mix suchstreams.

Since some styrenic polymers are either quite viscous or are solids atfeed temperatures, it is preferred that the second stream additionallyinclude a solvent capable of solubilizing the styrenic polymer. Also,for mass transfer reasons, it is preferred that the third stream includea liquid with which the catalyst can form a slurry, solution, suspensionor dispersion. The intimate mix formed by the mixer can be fed to areactor in which bromination and/or continued bromination of at least aportion of the styrenic polymer occurs.

By practicing the process of this invention in the above-describedmanner, several benefits are realized. First, by intimately mixing thethree streams in a mixer, the formation of large volumes of vapor andthe eruption of same are obviated. Second, it has been demonstrated thatby using a feed mixture formed from a brominating agent and a styrenicpolymer, the most active bromination catalyst can be used without havingto practice prior art techniques to hopefully protect againstcross-linking of the styrenic polymer. For example, so as to guardagainst cross-linking when AlCl₃ is the catalyst, there is no need topre-add bromine to the reactor as is taught in U.S. Pat. No. 4,975,496.Nor is there a need to add a Lewis base, e.g., water, to the reactionvessel to control cross-linking as is taught in U.S. Pat. No. 4,200,703.Nor is there a need to use a less active catalyst in an anhydrous systemto tame cross-linking as is taught in U.S. Pat. No. 4,352,909. Third, byforming a mixture from the brominating agent and styrenic polymerreactants, especially a homogenous mix, there is avoided concentrationanomalies which can give rise to the production of undesirableby-products. In prior art processes where bromine is added to a reactionmass of styrenic polymer and catalyst, there is an anomalous zone, inthe area of the bromine addition, in which the polymer sees anoverabundance of bromine. In the case of adding separate bromine andstyrenic polymer streams to a reactor containing a bromination catalyst,there will be two anomalous zones, one rich in bromine and the otherrich in polymer. By not having the correct stoichiometry in these zones,there are introduced opportunities for the formation of undesirableby-products.

DESCRIPTION OF THE DRAWING

FIG. 1 is a schematic diagram depicting a process of this invention.

DESCRIPTION OF THE INVENTION

Styrenic polymers which are brominated in accordance with the presentinvention are homopolymers and copolymers of vinyl aromatic monomers,that is, monomers having an unsaturated moiety and an aromatic moiety.The preferred vinyl aromatic monomers have the formula:

    H.sub.2 C═CR--AR

wherein R is hydrogen or an alkyl group having from 1 to 4 carbon atomsand Ar is an aromatic radical (including various alkyl andhalo-ring-substituted aromatic units) of from 6 to 10 carbon atoms.Examples of such vinyl aromatic monomers are styrenesalpha-methylstyrene, ortho-methylstyrene, meta-methylstyrene,para-methylstyrene, para-ethylstyrene, isopropenyltoluene,isopropenylnaphthalene, vinyl toluene, vinyl naphthalene, vinylbiphenyl, vinyl anthracene, the dimethylstyrenes, t-butylstyrene, theseveral chlorostyrenes (such as the mono- and dichloro-variants), theseveral bromostyrenes (such as the mono-, dibromo- andtribromo-variants). Polystyrene is the currently preferred styrenicpolymer and, when the styrenic polymer being brominated is a copolymerof two or more vinyl aromatic monomers, it is preferred that styrene beone of the monomers and that the styrene comprise at least 50 weightpercent of the copolymerizable vinyl aromatic monomers.

The styrenic polymers, which are brominated in accordance with thepresent invention, are readily prepared by bulk or mass, solution,suspension or emulsion polymerization techniques comparable to thoseemployed in the polymerization of styrene. Polymerization can beeffected in the presence of free radical, cationic or anionicinitiators, such as di-t-butyl peroxide, azo-bis(isobutyronitrile),di-benzoyl peroxide, t-butyl perbenzoate, dicumyl peroxide, potassiumpersulfate, aluminum trichloride, boron trifluoride, etherate complexes,titanium tetrachloride, n-butyllithium, t-butyllithium, cumylpotassium,1,3-trilithiocyclohexane, and the like. The polymerization of styrene,alone or in the presence of one or more monomers copolymerizable withstyrene, is well known and it is considered unnecessary to furtherdiscuss the polymerization process. The styrenic polymers having amolecular weight of at least 1,000, preferably at least 50,000 and mostpreferably 150,000 to 500,000, are brominated in accordance with thepresent invention. Although styrenic polymers outside these molecularweight ranges can be brominated in accordance with the presentinvention, there is typically no economic advantage in so doing.

The catalyst used in the processes of this invention can be anybromination catalyst, provided that the catalyst does not act tofrustrate the efficient and safe production of a high quality brominatedpolystyrenic product. The favored catalysts are the Lewis acid catalystswhich are typified by AlCl₃, FeCl₃, AlBr₃, FeBr₃, SbCl₅, ZrCl₄, and thelike. Fe, Al and Sb₂ O₃ may be used to form Lewis acid catalysts bysimply adding them to the reaction system. Mixtures of catalyst can alsobe used. Once the catalyst has been added to the reaction system, it mayundergo some reaction without significant loss of catalytic activity,e.g., AlCl₃ may convert to some extent to AlBr₃. The more preferredcatalysts are the aluminum and iron-based catalysts. Of these, the mostpreferred are the aluminum and iron halides, especially the bromides andchlorides. AlCl₃ and FeCl₃ are most highly preferred, with AlCl₃ beingthe catalyst of choice.

The catalyst is used in an amount which is sufficient to obtain thecatalytic effect sought. These catalytic amounts will depend on theactivity of the catalyst, but will generally fall within the range offrom about 0.2 to about 20 weight percent and preferably within therange of from about 0.5 to about 15 weight percent, based on the weightof the styrenic polymer being brominated. The most active catalysts willbe used in the lower amounts while the less active catalysts will beused in the higher amounts. For the preferred aluminum and iron-basedcatalysts, it is preferred that they be used in amounts within the rangeof from about 0.5 to about 5 weight percent. AlCl₃ and FeCl₃ are usefulin amounts within the range of from about 0.2 to about 10 weightpercent. When AlCl₃ is the catalyst, amounts within the range of fromabout 0.5 to about 3 weight percent are preferred.

The brominating agents useful in the process of this invention can beany of those which can brominate aromatic carbons in the polymer's vinylaromatic units (hereinafter also referred to as styrenic monomer units).The art recognizes Br₂ and BrCl as good brominating agents, with theformer being most preferred. Bromine can be obtained commercially in thediatomic form or can be generated by the oxidation of HBr. Br₂ can besupplied either as a liquid or a gas. The amount of brominating agentused in the process should provide an overall mole ratio of totalbrominating agent to total styrenic polymer fed, which will provide from1 to 3 bromine substitutions per styrenic monomer unit in the polymer.Generally, it is desired that the brominated styrenic polymer productsof this invention contain at least 30 wt % bromine, based upon the totalweight of the brominated polymer. It is preferred that the brominatedpolymer contain above about 50 wt % bromine and most preferably aboveabout 60 wt % bromine. For any particular styrenic polymer, the amountof brominating agent used in the process will be determined by thebromine content desired considering the highest bromine content which isobtainable with the process parameters chosen. The higher brominecontents will require the most brominating agent. It is pointed out thatas perbromination is approached, it becomes more difficult to substitutethe last bromines. Adding ever larger amounts of brominating agent doesnot always attenuate this difficulty. However, it is helpful, inattempting to maximize the bromine content, to provide a smallstoichiometric excess of brominating agent. Stoichiometric excesses upto about 10% are preferred. The stoichiometry is easily determined as itrequires one mole of Br₂ or BrCl per substitution sought. In practice,the practitioner will determine the bromine content sought on a weightbasis and then will calculate, on an idealized basis, the number ofmoles of brominating agent needed to obtain the same. For example, ifthe styrenic polymer is polystyrene and the bromine content sought is 68wt %, at least 2.7 moles of bromine or BrCl per styrene monomer unitwill be required, not including any desired stoichiometric excess. Forbrominated polystyrene, a bromine content of from about 40 to about 70+wt % bromine is desirable. This range can be theoretically obtained witha mole ratio of bromine to styrene monomer of from about 0.9:1 to about3.0:1 Preferred for brominated polystyrene is a bromine content of fromabout 60 to about 70+ wt %, which can be obtained with a theoreticalmole ratio of from about 1.9:1 to about 3.0:1 for bromine or BrCl. Theprocesses of this invention can, with facility, provide up to 70 wt %,say 67-68 wt %, bromine. In determining the amount of brominating agentin the process, the brominating agent in the feed mixture and anybrominating agent pre-added prior to the feed of the mixture are bothcounted. As pointed out herein, it is not necessary to pre-add abrominating agent to the catalyst and, thus, all of the processbrominating agent requirements can be supplied via the feed of themixture. If, however, the practitioner chooses to pre-add a brominatingagent to the reactor, it can be done.

While the foregoing describes the overall quantitative relationshipbetween the brominating agent and styrenic polymer, the quantitativerelationship between these two reactants in the feed mixture has notbeen fully discussed. Generally, the mixture which is to be fed willcontain from about 1 to about 8 moles of brominating agent per mole ofstyrenic monomer units and from about 0.5 to about 20 wt % ofbromination catalyst per weight of styrenic polymer during the feedperiod. During the feed, the quantitative relationship can be constantor can vary within the above-mentioned range. (It is within the scope ofthis invention to allow for some excursions outside of the range so longas such does not do significant harm to the process efficiency or toproduct quality.) A preferred range is from about 2.5 to about 5 molesof brominating agent per mole of styrenic monomer units and from about0.5 to about 5 wt % bromination catalyst per weight of styrenic polymerin the feed mixture. As can be appreciated, the use of an amount ofbrominating agent in the feed mixture which gives a mole ratio ofbrominating agent to styrenic monomer units which is less than orgreater than the selected overall mole ratio of brominating agent tostyrenic monomer units, will result in exhaustion of either thebrominating agent or the styrenic polymer in forming the intimatemixture before exhaustion of the other constituent. For example, if thepractitioner chooses to produce brominated polystyrene with a 70 wt %bromine content, an overall molar ratio of bromine to styrenic monomerunits of 3.0:1, and any excess if desired, would be suitable. If thepractitioner chooses to form a feed mixture in which the molar ratio ofbromine to styrenic monomer units is 1:1, it can be seen that the amountof polystyrene to be fed will be completed before obtaining the neededoverall amount of bromine. In this case, the practitioner first uses the1:1 mixture and then continues on with just a bromine feed after thepolystyrene feed has been exhausted. If, on the other hand, the molarratio in the feed mixture is chosen to be 5:1, then the bromine willfirst become exhausted and the formation of the intimate mixture willhave to be finished with the polystyrene and bromination catalyst alone.Generally, it is preferred to have the overall molar ratio and the feedmixture ratio at least somewhat similar. In all cases though, theinitial feed should preferably contain at least a molar ratio of bromineto styrenic monomer units of 1:1.

It is preferred that the bromine used in the process of this inventionbe essentially anhydrous, i.e., contain less than 100 ppm (weight basis)water and contain no more than 10 ppm organic impurities, e.g., oil,grease, carbonyl containing hydrocarbons, iron, and the like. Available,commercial grade bromine may have such purity. If, however, such is notavailable, the organic impurities and water content of the bromine canbe conveniently reduced by mixing together a 3 to 1 volume ratio ofbromine and concentrated (94-98 percent) sulfuric acid. A two-phase mixis formed which is stirred for 10-16 hours. After stirring and settling,the sulfuric acid phase, along with the impurities and water, isseparated from the bromine phase. To further enhance the purity of thebromine, the recovered bromine phase can be subjected to distillation.

As before stated, it is preferred that the processes of this inventionuse a solvent. The solvent must be capable of solubilizing the styrenicpolymer feed and be relatively inert to the process at reactionconditions. The solvent should also exhibit solubility of theunderbrominated styrenic polymers and, in preferred cases, the finalbrominated product. Preferred solvents are those in which thebromination catalyst is also soluble, readily dispersed or readilysuspended. Halogenated solvents are preferred and are exemplified bycarbon tetrachloride, chloroform, tetrachloroethane, methylene chloride,dichloroethane, trichloroethylene, trichlorobenzene, methylene bromide,1,2-dibromoethane, dichlorodifluoromethane, bromochloromethane, andmixtures thereof. Especially preferred are bromochloromethane,1,2-dichloroethane, and methylene chloride.

By forming a solution of solvent and styrenic polymer, the polymerbecomes easy to handle and facile in forming the intimate mix. Thesolutions of this invention preferably contain from about 5 to about 50wt % polymer. More highly preferred are those which contain from about 5to about 30 wt % polymer.

It is preferred to have the bromination catalyst to be in associationwith a liquid so that the catalyst can be in a slurry, solution,dispersion or suspension. Such will enhance reaction mass mixing andmass transfer qualities. It is expedient, but not necessary, to use thesame liquid, i.e., solvent, that is used to form the styrenic polymersolution. Thus, in a preferred mode, processes of this invention willprovide a mixture of halogenated solvent and catalyst which can beeasily pumped to the mixer. The mixture of liquid and catalyst is bestdescribed as a suspension. Generally, the suspension will be from about95 to about 99.8 wt % liquid and preferably from about 99 to about 99.8wt %, based on the total weight of liquid and catalyst.

The solvent used to dissolve the styrenic polymer and the liquid used inassociation with the catalyst are preferably dry, that is, they containless than about 200 ppm (weight basis) water between them and preferablyless than about 150 or 100 ppm water. The presence of water is notdesired as, in significant quantities, it can deactivate the catalyst toan undesirable extent. If, for some reason, the practitioner has largeamounts of water in the process and dewatering is not practical, then itmay be possible to overcome the situation by simply increasing theamount of the catalyst used For the process of this invention, it is nota feature to solely use water to avoid cross-linking as is taught inU.S. Pat. No. 4,200,703--but rather, this invention attenuatescross-linking by means which include its novel feeding technique.

The feed of the three streams should occur expeditiously, withconsideration being give to the ability of the process equipment tohandle the heat load from the exothermic bromination process, theevolving HBr, and other process concerns. In short, the feed can occurover the shortest time period that will be allowed by the equipmentwithout excursion outside of the critical process parameters. Generally,it is anticipated that the feed period will be from 0.5 to 3 hours for acommercial-size plant. Shorter feed periods are expected for smallerscale processes.

The process of this invention occurs at a temperature within the rangeof from about -20° to about 60° C. and preferably within the range offrom about 0° to about 10° C. The pressure can be atmospheric,subatmospheric or superatmospheric.

To carry out a process of this invention, a bromination catalyst, sayAlCl₃, is suspended with essentially anhydrous bromochloromethane togive an easily stirrable suspension. This suspension is fed to aglass-lined, stirred reactor having an exterior loop and brought to atemperature within the range of from about -5° to about 10° C. Thesuspension is kept under an inert, dry atmosphere in the reactor. Asolution of a styrenic polymer and solvent, e.g., bromochloromethane, isprepared. From the reactor is withdrawn a stream which is initiallycomprising the suspended catalyst. The suspended catalyst stream, astream of the styrenic polymer solution and a stream of the brominationagent are fed to a mixer located in-line with the exterior loop. Withinthe mixer is formed an intimate mixture of the three streams. Somebromination may occur in the mixture as it is returned back to thereactor to form a part of the reactor contents. The process continuesuntil all of the brominating agent and styrenic polymer have been fed.As the process continues, the degree of bromination of the polystyrenewill increase.

Exemplifying the use of an exterior reactor loop, reference is made toFIG. 1 wherein there is shown a reactor generally designated by thenumeral 1. Reactor 1 is a stirred reactor and initially contains acatalyst charge and a solvent, say any of the preferred halogenatedhydrocarbon solvents. Reactor discharge conduit 4 provides a stream fromreactor 1 which is fed to pump 5. Pump 5 pressurizes the stream so thatit is fed with force via conduit 7 to impingement mixer 10. Bromine isfed via conduit 20 to pump P₁ and thence, via conduit 21 to impingementmixer 10. A solution of polystyrene and solvent (preferably the samesolvent as that which is in reactor 1) is fed via conduit 22 to pump P₂and then on to impingement mixer 10 via conduit 23. In mixer 10 thethree streams are formed into an intimate mixture. The discharge fromimpingement mixer 10 is fed via conduit 33 to reactor 1 through feedport 3. The removal of contents from reactor 1 and their feed toimpingement mixer 10 continues to occur until at least substantially allof the bromine and polystyrene/solvent solution have been fed.

As can be appreciated, the contents of reactor 1 change in compositionduring the bromine and polystyrene/solvent solution feeds. Initially,the contents of reactor 1 comprise catalyst and solvent. As the processruns, the reactor contents comprise and begin to become more rich inbrominated polystyrene, some of which is underbrominated and some ofwhich is of the degree of bromination sought. During a cook period, thefinal bromination occurs. Continued routing of a reactor stream throughthe exterior loop can continue during the cook period to aid in mixing.

As pointed out earlier, the bromination of styrenic polymers is asubstitution reaction. The main by-product from this reaction is HBr.The HBr formed in the process is usually found in the head space abovethe reactor contents. It is preferred that the HBr be removed and passedto a water scrubber or be stored as dry HBr. A dry inert gas saynitrogen, can be used as a pad over the reactor contents to minimize thepresence of water therein.

The reactor is kept at a low temperature, e.g., from about 0° to about10° C., during the feed of the styrenic polymer and/or brominating feed,as the case may be, and preferably from about 4° to about 8° C.

After the feed is accomplished, the reactor is maintained for a cookperiod of from about 0.5 to about 6 hours and preferably from about 1 toabout 3 hours. The cook temperature is within the range of from about 0°to about 10° C. and preferably within the range of from about 2° toabout 5° C. The cook period serves to continue the bromination until thesought degree of bromination is obtained. It may be for a long period ifthe reaction parameters provide for mild bromination conditions duringthe bromine and polystyrene feeds or it may be for a short period if theparameters chosen provide for more severe bromination conditions. Thecook period generally occurs in the reactor.

After the cook period, the reaction mass can be treated with water,sodium sulfite, sodium gluconate, and sodium hydroxide to deactivate thecatalyst, kill any remaining brominating agent, and to adjust thereaction mass pH. After these treatments, the reaction mass is settledto obtain a two-phase reaction mass containing an organic phase, whichcontains, as a solute, the brominated styrenic polymer product and anaqueous phase. The aqueous phase is decanted and the remaining organicphase is stripped of its solvent component. It is most convenient toaccomplish this strip by pouring the organic phase into boiling water.As the solvent is stripped, the brominated styrenic polymer productforms a precipitate. The precipitate can be recovered by anyliquid-solid separation technique, e.g., filtration, centrifugation,etc. The recovered precipitate is then dried.

The brominated styrenic polymers of this invention are suitable for useas flame retardants in thermoplastics, especially engineeringthermoplastics, e.g., polybutylene terephthalate, polyethyleneterephthalate, nylon and the like. These brominated polymers are used inflame retarding quantities, say from about 5 to about 20 wt % brominatedpolymer per hundred weight of thermoplastic. Conventional blendingtechniques can be used as taught in the prior art. In addition,conventional additives, such as UV stabilizers, impact modifiers, flameretardant synergists, dyes, pigments, fillers, plasticizers, flow aids,antioxidants, free radical initiators, and the like may be used as theneed requires.

What is claimed:
 1. A process for the bromination of polystyrene, whichprocess comprises:a. providing a bromination catalyst and associatedliquid in a reactor and feeding a portion of the bromination catalystand associated liquid to a mixer external of the reactor; b. feeding abrominating agent and a solution of polystyrene as separate streams tothe external mixer, in which:i. the separate streams, prior to being fedto the external mixer, are substantially free of a bromination catalyst;ii. the solvent used in forming the polystyrene solution and the liquidassociated with the catalyst contains less than 200 ppm water betweenthe two of them; and iii. the brominating agent contains less than about100 ppm water.
 2. The process of claim 1 wherein the solution solventand the associated liquid are the same.
 3. The process of claim 1wherein the solution solvent is chosen from the group consisting ofbromochloromethane, 1,2-dichloroethane and methylene chloride.
 4. Theprocess of claim 1 wherein the solution solvent is bromochloromethane.5. The process of claim 1 wherein the brominating agent is bromine. 6.The process of claim 1 wherein the bromination catalyst is an aluminumor iron-based catalyst or a mixture of any of them.
 7. The process ofclaim 1 wherein the bromination catalyst is an aluminum or iron halideor a mixture of any of them.
 8. The process of claim 1 wherein thebromination catalyst is an aluminum or iron-based catalyst or a mixtureof any of them and wherein the catalyst is used in an amount which iswithin the range of from about 0.5 to about 5 weight percent, based onthe weight of the styrenic polymer being brominated.
 9. The process ofclaim 1 wherein the bromination catalyst is AlCl₃ or FeCl₃ or a mixtureof them and wherein the catalyst is used in an amount within the rangeof from about 0.2 to about 10 weight percent, based on the weight of thestyrenic polymer being brominated.
 10. The process of claim 1 whereinthe bromination catalyst is AlCl₃ and wherein the catalyst is used in anamount within the range of from about 0.5 to about 3 weight percent,based on the weight of the styrenic polymer being brominated.
 11. Theprocess of claim 1 wherein the solution solvent is bromochloromethane,the bromination catalyst is AlCl₃ and wherein the catalyst is used in anamount within the range of from about 0.2 to about 10 weight percent,based on the weight of the styrenic polymer being brominated.
 12. Theprocess of claim 11 wherein the amount of catalyst used is within therange of from about 0.5 to about 3 weight percent, based on the weightof the styrenic polymer being brominated.